US4045960A - Process for producing energy - Google Patents

Process for producing energy Download PDF

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Publication number
US4045960A
US4045960A US05/647,965 US64796576A US4045960A US 4045960 A US4045960 A US 4045960A US 64796576 A US64796576 A US 64796576A US 4045960 A US4045960 A US 4045960A
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United States
Prior art keywords
gas
methanol
synthesis
exhaust gas
partial stream
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Expired - Lifetime
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US05/647,965
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English (en)
Inventor
Gerhard Cornelius
Friedemann Marschner
Emil Supp
Toma Varlam
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GEA Group AG
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Metallgesellschaft AG
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
    • F02C6/04—Gas-turbine plants providing heated or pressurised working fluid for other apparatus, e.g. without mechanical power output
    • F02C6/10—Gas-turbine plants providing heated or pressurised working fluid for other apparatus, e.g. without mechanical power output supplying working fluid to a user, e.g. a chemical process, which returns working fluid to a turbine of the plant

Definitions

  • This invention relates to a process of producing or recovering energy, particularly of producing electric energy, by the utilization of the pressure and heat potentials of exhaust gases formed in chemical syntheses, particularly in the synthesis of methanol.
  • German Pat. No. 2,013,297 describes a process in which the reaction heat is utilized which is generated when methanol is produced from a synthesis gas which contains carbon oxides and hydrogen and which has been produced by a cracking of hydrocarbons by a treatment with water vapor on an indirectly heated, nickel-containing catalyst at temperatures above 700° C, and which synthesis gas is reacted on a copper-containing catalyst under pressures of 30-80 kg/cm 2 and at temperatures of 230°-280° C.
  • the latter catalyst is contained in tubes which are indirectly cooled with water with production of high-pressure steam.
  • the resulting high-pressure steam can be expanded to a back-pressure of 4-6 kg/cm 2 with performance of work, and the remaining low-pressure steam may be used to supply heat to the final distillation of the methanol which has been produced.
  • Some syntheses involve a formation of exhaust gases which contain not only sensible heat but are under the pressure under which the synthesis has been effected. This pressure may amount, e.g., in the synthesis of methanol, to 200 bars (German Pat. No. 1,668,390) and has not yet been utilized for a production of energy.
  • This invention utilizes the sensible heat contained in the exhaust gases formed in such and similar reactions as well as the energy which is due to the existing pressure. For instance, in the synthesis of methanol, the sensible heat and the pressure energy of the exhaust gas and the sensible heat of the product gas, which is the gas leaving the synthesis reactor, have not been utilized in the lower temperature region but have been transferred to the air or cooling water. It is also an object of the invention to improve the economy of chemical syntheses and to reduce the cost of the resulting end product in that energy is produced or recovered from exhaust gases which are worth-less otherwise.
  • FIG. 1 is a flow diagram of one embodiment of the process according to the invention.
  • FIG. 2 is a flow diagram of another embodiment of the process according to the invention.
  • the exhaust gas is partly expanded with performance of work and is then re-overheated as a counterflow to the product gas and is subsequently expanded further.
  • the exhaust gas is heated by extraneous heat.
  • This extraneous heat may consist of the waste heat from other chemical processes or plants, or the exhaust gas may be heated in a manner known per se in a furnace.
  • the advantages afforded by the invention reside particularly in that the sensible heat and/or the pressure of exhaust gases formed in chemical processes, such as catalytic reactions of gases which contain CO, CO 2 , and H 2 , are utilized for a production of energy.
  • the invention is applicable to all chemical syntheses in which exhaust gases are formed, particularly to the synthesis of methanol. It makes no difference from which raw material the methanol is produced.
  • solid fuels such as coal
  • liquid fuels such as hydrocarbon oils, gasolines, and the like
  • gaseous raw materials such as natural gas or suitable synthesis gases.
  • the process is simple and inexpensive and does not require any or any substantial supervision. It is particularly desirable in conjunction with processes in which exhaust gases are formed at high rates.
  • 1 designates the fresh gas inlet, 2 the compressor for recycled gas, 3 a conduit for recycled gas, 4 the heat exchanger for the recycled synthesis gas and the product gas, 5 the methanol synthesis reactor, 6 an exhaust gas preheater, 7 an air cooler, 8 a final cooler with an inlet 9 and an outlet 10 for the coolant, 11 a methanol separator, 12 an exhaust gas conduit, 13 another exhaust gas preheater, 14 a generator, 15 an expansion turbine, and 16 an outlet for raw methanol.
  • fresh gas for the synthesis of methanol is supplied at 1.
  • This gas may be produced by a suitable treatment of coal, naphta, natural gas, etc.
  • the fresh gas is produced from a natural feed gas in a steam reforming plant, and has the following constituents in % by volume:
  • the fresh gas is under a pressure of 5-40 bars.
  • the fresh gas is compressed by means of a compressor to the reaction pressure required for the methanol synthesis, in the present case to about 80 bars.
  • a compressor 2 for recycled gas is operated to maintain an optimum ratio in the present case preferably 3:1, of recycled gas to fresh gas.
  • This recycled gas is fed through 3 into the heat exchanger 4 and in the latter is conducted as a counterflow to the product gas and is thus heated to the temperature of 190°-280° C required at the inlet of the methanol synthesis reactor 5. In the latter, CO, CO 2 and H 2 are partly reacted to methanol.
  • the product gas leaving the methanol synthesis reactor 5 contains 6.1 % by volume methanol and 1.6 % by volume water and delivers its sensible heat and part of its heat of condensation in the parallel-connected heat exchanger 4 and exhaust gas preheater 6 to the recycled gas and exhaust gas, respectively.
  • the exhaust gas preheater 6 may be connected parallel to and/or in series with the heat exchanger 4 so that the exhaust gas can be simply overheated, or re-overheated.
  • the product gas is further cooled in an air cooler 7 or in a final cooler 8 or only in a final cooler 8 to a temperature which depends on the coolant temperature and in the present case amounts to 45° C.
  • the raw methanol which is condensed out is separated from the remaining gas in the methanol separator 11 and is removed from the process at 16. A major portion of the remaining gas is mixed with fresh gas and the cycle begins anew.
  • exhaust gas part of the residual gas must be removed from the cycle. This part of the residual gas will be referred to as exhaust gas hereinafter.
  • the pressure may amount to between 25 and 150 bars, depending on the selected reaction pressure, and in the present case amounts to 80 bars. If fresh gas 1 is supplied at a rate of 361,115 standard m 3 /h, the reaction performed as stated above will result in a production of exhaust gas at a rate of 107,244 standard m 3 /h.
  • the exhaust gas is now heated to a temperature level between 50°and 265° C, in the present case to 200° C, in a flow path which is connected in series with and/or parallel to the product gas. This temperature level depends on the reaction pressure and the final reaction temperature.
  • the flow of the exhaust gas in the exhaust conduit 12 and the exhaust gas preheater 6 results in a pressure loss so that the exhaust gas enters the expansion turbine 15 in the present case under a pressure of 76 bars.
  • the exhaust gas can be expanded to a pressure between 75 bars and 1 bar with performance of work.
  • the gas is expanded to a pressure of 3 bars, corresponding to an outlet temperature of 5° C, if the expansion turbine 15 has an efficiency of 72.5%.
  • the energy produced in the expansion turbine 15 may drive a directly coupled machine or may be transformed into electric energy in a directly coupled generator.
  • the exhaust gas may be alternatively expanded in two stages. After the first stage the exhaust gas is indirectly returned to the cycle and is re-overheated.
  • the electrical energy produced in the present case is calculated as follows.
  • Example 2 differs from Example 1 in that the exhaust gas is not heated in the cycle but is heated in a fired overheater.
  • the overheater may be fired with part of the exhaust gas as well as with fossile fuels which are extraneous to the process.
  • the exhaust gas may alternatively be heated by hot fluids, such as superheated steam.
  • the exhaust gas at a rate which becomes available under the same conditions may be heated to a temperature between 50° and 500° C. in a fired overheater, in the present case preferably to 200° C.
  • the exhaust gas is then expanded to 20 bars in the first expansion stage of the expansion turbine and is again supplied to the overheater for being re-overheated to 200° C.
  • the gas is subsequently expanded further to 2 bars.
  • the overheated exhaust gas may alternatively be expanded directly to the final pressure of 2 bars.
  • the generator 14 produces an electric power of 10,539 kW.
  • the electric energy produced in this case is calculated as follows:

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US05/647,965 1975-01-15 1976-01-09 Process for producing energy Expired - Lifetime US4045960A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19752501377 DE2501377A1 (de) 1975-01-15 1975-01-15 Verfahren zur energieerzeugung
DT2501377 1975-01-15

Publications (1)

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US4045960A true US4045960A (en) 1977-09-06

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ID=5936483

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US05/647,965 Expired - Lifetime US4045960A (en) 1975-01-15 1976-01-09 Process for producing energy

Country Status (7)

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US (1) US4045960A (ro)
CA (1) CA1037265A (ro)
DE (1) DE2501377A1 (ro)
FR (1) FR2298002A1 (ro)
IT (1) IT1054937B (ro)
NL (1) NL7512364A (ro)
RO (1) RO66216A (ro)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4224299A (en) * 1978-11-02 1980-09-23 Texaco Inc. Combination chemical plant and Brayton-cycle power plant
US4239693A (en) * 1979-06-22 1980-12-16 Foster Wheeler Energy Corporation Process for production of methanol
US4273743A (en) * 1978-11-02 1981-06-16 Texaco Inc. Combination chemical plant and Brayton-cycle power plant
US4288406A (en) * 1979-08-29 1981-09-08 Exxon Research & Engineering Co. Process energy recovery
FR2495606A1 (fr) * 1980-12-05 1982-06-11 Foster Wheeler Energy Corp Procede pour produire un produit de reaction brut, par exemple du methanol, par recuperation des gaz de vidange de l'etape de synthese
US6641625B1 (en) 1999-05-03 2003-11-04 Nuvera Fuel Cells, Inc. Integrated hydrocarbon reforming system and controls
US6986797B1 (en) 1999-05-03 2006-01-17 Nuvera Fuel Cells Inc. Auxiliary reactor for a hydrocarbon reforming system
US7066973B1 (en) 1996-08-26 2006-06-27 Nuvera Fuel Cells Integrated reformer and shift reactor
US20070006566A1 (en) * 2005-07-05 2007-01-11 General Electric Company Syngas turbine
US7507384B2 (en) 2002-06-13 2009-03-24 Nuvera Fuel Cells, Inc. Preferential oxidation reactor temperature regulation
CN109268092A (zh) * 2018-08-02 2019-01-25 上海柯来浦能源科技有限公司 一种利用空气能源的氢气混合工质动力系统

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0753652A1 (en) * 1995-07-10 1997-01-15 N.V. Kema Synthesis of ethene

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1583621A (en) * 1924-03-20 1926-05-04 Steinberg Reuben Automobile exhaust generator propulsion
US2303381A (en) * 1941-04-18 1942-12-01 Westinghouse Electric & Mfg Co Gas turbine power plant and method
US3296449A (en) * 1963-02-19 1967-01-03 Bbc Brown Boveri & Cie Process for the production of electrical energy from the chemical energy of fuels
US3928973A (en) * 1974-08-12 1975-12-30 Mintech Corp Process for extracting water and energy from synthesis gas
US3959972A (en) * 1974-05-30 1976-06-01 Metallgesellschaft Aktiengesellschaft Power plant process

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2955917A (en) * 1958-05-13 1960-10-11 Edward S Roberts Process and apparatus for the manufacture of nitric acid at elevated pressures with full power recovery
DE1104973B (de) * 1958-12-22 1961-04-20 Hellmuth Walter Verfahren und Vorrichtung zum Antrieb hauptsaechlich von Unterwasserfahrzeugen

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1583621A (en) * 1924-03-20 1926-05-04 Steinberg Reuben Automobile exhaust generator propulsion
US2303381A (en) * 1941-04-18 1942-12-01 Westinghouse Electric & Mfg Co Gas turbine power plant and method
US3296449A (en) * 1963-02-19 1967-01-03 Bbc Brown Boveri & Cie Process for the production of electrical energy from the chemical energy of fuels
US3959972A (en) * 1974-05-30 1976-06-01 Metallgesellschaft Aktiengesellschaft Power plant process
US3928973A (en) * 1974-08-12 1975-12-30 Mintech Corp Process for extracting water and energy from synthesis gas

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4224299A (en) * 1978-11-02 1980-09-23 Texaco Inc. Combination chemical plant and Brayton-cycle power plant
US4273743A (en) * 1978-11-02 1981-06-16 Texaco Inc. Combination chemical plant and Brayton-cycle power plant
US4239693A (en) * 1979-06-22 1980-12-16 Foster Wheeler Energy Corporation Process for production of methanol
US4288406A (en) * 1979-08-29 1981-09-08 Exxon Research & Engineering Co. Process energy recovery
FR2495606A1 (fr) * 1980-12-05 1982-06-11 Foster Wheeler Energy Corp Procede pour produire un produit de reaction brut, par exemple du methanol, par recuperation des gaz de vidange de l'etape de synthese
US7066973B1 (en) 1996-08-26 2006-06-27 Nuvera Fuel Cells Integrated reformer and shift reactor
US6641625B1 (en) 1999-05-03 2003-11-04 Nuvera Fuel Cells, Inc. Integrated hydrocarbon reforming system and controls
US6986797B1 (en) 1999-05-03 2006-01-17 Nuvera Fuel Cells Inc. Auxiliary reactor for a hydrocarbon reforming system
US7507384B2 (en) 2002-06-13 2009-03-24 Nuvera Fuel Cells, Inc. Preferential oxidation reactor temperature regulation
US20070006566A1 (en) * 2005-07-05 2007-01-11 General Electric Company Syngas turbine
CN109268092A (zh) * 2018-08-02 2019-01-25 上海柯来浦能源科技有限公司 一种利用空气能源的氢气混合工质动力系统

Also Published As

Publication number Publication date
RO66216A (ro) 1980-03-15
DE2501377A1 (de) 1976-07-22
FR2298002B1 (ro) 1982-10-22
NL7512364A (nl) 1976-07-19
FR2298002A1 (fr) 1976-08-13
IT1054937B (it) 1981-11-30
CA1037265A (en) 1978-08-29

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